Liquid mixing employing expanding thinning liquid sheets

ABSTRACT

Two or more liquids are mixed continuously in very short times and in a highly uniform manner. Thin sheets of the liquids to be mixed are formed and contacted to produce a new mixed sheet. The newly formed mixed sheet is highly turbulent which substantially enhances mixing. Since the contacting of the liquids occurs on a scale of microns of thickness, mixing is not only rapid but complete and extremely uniform as well. Turbulence within the mixed sheet that further enhances mixing allows for mixing times as low as 0.1 millisecond, depending on flowrate and pressure drop, for low viscosity fluids.

BACKGROUND

1. Field of the Invention

This invention relates to rapid and complete mixing of fluids in acontinuous manner by a process that mixes very thin liquid sheets of thedifferent fluids together.

2. Description of Prior Art

The prior art has been concerned for many years with the rapid andcomplete mixing of liquids so as to reduce segregation of componentswithin the mixture. Less than very rapid and complete dispersion isparticularly deleterious in processes utilizing very fast reactions. Theterm fast reaction implies a reaction that has a time scale that is morerapid or on the same order of the time scale of mixing of the reactants.If the fast reactions are complex, i.e., they involve reactions that aremultistep, then product distribution can be adversely affected (see J.Y. Oldshue, Fluid Mixing Technology, McGraw-Hill Publications Co., NewYork, N.Y., 1983, pp. 222-229). Segregation that occurs due toinhomogeneities within the mixture on the molecular scale can change theproduct distribution from that calculated assuming perfect and completemixing before the reactions, begin, Particularly with multiple reactionsfailure to pay attention to segregation within the mixture can causewastage of raw materials in producing undesired substances, difficultiesin scale-up, and an increased load on the separation plant (see J. R.Bourne, F. Kozicki, and P. Rys, "Mixing and Fast Chemical Reaction",Chem. Eng. Sci., 36 (10), pp. 1643-1663, 1981).

In general, liquid phase reactions occuring in viscous media, such aspolymerization and biochemical reactions, are particularly subject tothe influence of segregation. A recent symposium "Rapid Mixing andSampling Techniques in Biochemistry" explained the problems ofcharacterizing biochemical reactions that proceeded more rapidly thanthe time scale of the initial mixing of the reactants (see Chance, B.,et. al. (eds.), Rapid Mixing and Sampling Techniques in Biochemistry,Academic Press, New York, N.Y., 1964).

Prior art for rapid mixing generally uses jets of liquid that impingeagainst one another or tangentially mounted feed tubes that mix thefluids in a swirl cup. An example of such a mixing device is given inU.S. Pat. No. 4,239,732, granted Dec. 16, 1980 to W. Schneider. Thesetypes of mixers can give fairly complete mixing of very small amounts ofliquids in times as low as milliseconds for low viscosity fluids.However, these streams are relatively thick and this limits the speedwith which solutions can be mixed. It has long been known that if two ormore liquids can be made as thin as possible before they are mixed, thenrapid and complete mixing is virtually assured (see p. 49-53 in Chance,B. et. al., supra).

To this end a Russian scientist, Yu B. Kletenik in the Russian Journalof Physical Chemistry, Vol. 37(5), p. 638 (May, 1963) has devised amixing device that mixes thin liquid layers together. It does this byflowing two liquids between very narrow parallel plates similar to atriple decker sandwich. Between the first two plates the first fluidflows and between the second and third plate the second fluid flows. Theliquids are accelerated to high velocities (two meters/second orhigher), so that they flow separately through the parallel plates, andare mixed once they flow beyond the end of the plates and into freespace. With this system Kletenick claims to have obtained mixing timeson the order of 90 to 100 microseconds for low viscosity liquid sheetsof 200 microns thickness.

Although Kletenick claims that his device provides fast mixing, itsuffers from a number of drawbacks.

(1) Since the device requires flow between two parallel flat plates witha very narrow gap and of significant length, the pressure drop isrelatively high. Any attempt to further decrease the size of the thinfilm produced further increases the pressure drop. This is particularlysevere if the reactants are viscous.

(2) The width of the plates themselves must also be very thin (100microns), otherwise the fluids will completely miss each other once theyflow out the end of the narrow gaps. Such a device is not only difficultto construct but is also very delicate, rendering it unsuitable forindustrial use. Applications where the fluids must be injected at onlymoderately high pressures are not feasible.

(3) The device is limited to a gap of about 0.1 mm between plates whichlimits the thinness of the sheets formed to 0.2 mm or 200 microns as perKletenick's analysis of how his mixing device works.

(4) Because of the very narrow plate gaps plugging is a potentialproblem in systems containing suspended solids.

(5) Kletenick's device is impractical at usual industrial flowrates ofliters per minute and higher.

SUMMARY AND OBJECTS OF THE INVENTION

It has now been surprisingly found that the very thin liquid sheetsformed from liquid atomizers prior to droplet formation can be contactedor impinged at one another to produce a thin liquid mixed sheet. Theresult is surprising because such thin sheets (25 microns and less) aregenerally subject to disruption if they are contacted. However, if thesheets are contacted together in the same general direction of flow, andif a gentle angle of approach between the thin sheets is used, then thesheets will mix together and produce a new sheet of the mixture that ishighly turbulent.

It is one object of the present invention to provide a means ofcontacting two or more liquids in a sheet thinner than has heretoforebeen possible, yet at flowrates suitable for industrial use. As thecontacting of fluids occurs in thinner and thinner sizes, the mixingbecomes more complete as well as rapid. The thinner the physical scaleof mixing, the faster components can diffuse towards each other.

It is another object of the present invention to not only contact thinliquid sheets together, but further to mix them through turbulencewithin the newly-formed liquid sheet. This enhances mixing many fold byproviding bulk movement of liquids towards one another rather thanrelying on molecular diffusion along

It is also an object of the present invention to provide a means ofmixing liquid sheets together for fluids that are significantly viscouswithout unreasonable pressure drop.

A further object of the present invention is to provide devices formixing thin liquid sheets together that are very simple and easilymanufactured. The preferred embodiments of the present invention aresimple to manufacture, easy to maintain, and require no alignment tomaintain mixing of the ultra thin liquid sheets.

Readers will find further objects and advantages of the invention from aconsideration of the ensuing description and the accompanying drawings.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 illustrates the method by which a liquid atomizer forms a thinliquid sheet prior to droplet formation.

FIG. 2 is a sectional view of a preferred liquid atomizing device foruse in the present invention.

FIG. 3 illustrates a preferred embodiment of the present invention.

FIG. 4 illustrates other atomizing devices for use in the presentinvention.

DESCRIPTION OF A PREFERRED EMBODIMENT

FIG. 1 illustrates a swirl atomizer that generates droplets by thedisruption of a liquid sheet. Liquid 10 enters chamber 12 where it isswirled. The swirled liquid flows at high velocity (greater than 0.5meter/sec) as a thin film 11 with an air core 16 along the walls of theatomizer 14 until finally ejected into free space as a continuous thinliquid sheet 18. At some distance beyond the atomizer the sheet breaksup into droplets 20. Because the liquid velocity and liquid flowratewithin the sheet are constant (therefore, the cross sectional area mustremain constant), but the sheet expands radially or in its width, theliquid sheet must thin. This thinning continues to occur until surfacetension forces exceed inertial, forces causing the liquid to roll backon itself to form droplets 20. These sheets are very thin (of ordermicrons) and have a residence time on the order of milliseconds. Thesheets are stable, provided that they are not prematurely disrupted intoforming droplets. The droplets that form are typically 100 times or sothicker than the liquid sheet.

A preferred atomizer for practicing the present invention is shown inFIG. 2. Referring to FIG. 2, atomizer 30 swirls fluid 32 in core 34. Theswirled fluid flows along the walls of atomizer 30 as a fairly thinliquid layer of order hundreds of microns in thickness. The liquid sheet42 exits through opening 36 at an angle of about 110 to 150 degrees. Thecenter of atomizer 30 contains a deflector plate 38 that is screwed intothe very center of the atomizer on thread 40. The liquid sheet 42exiting the atomizer is deflected by deflector 38 to an angle of about120 to 170 degrees, preferably 150 degrees relative to the atomizer.

FIG. 3 illustrates how two of the atomizers considered in FIG. 2 can beused to practice the present invention. Atomizer 30 is now joined by anexact duplicate atomizer 60 that is inverted. Liquid sheets 42 and 62are formed at angles of 150 degrees relative to atomizer 30 and atomizer60 respectively. As the atomizers are brought physically closer to oneanother the liquid sheets 42 and 62 begin to contact and mix into a newsheet 72. As shown in FIG. 3, these single sheets are conical, resultingin a circular mixed sheet. The mixed sheet 72 is typically of equallength as either single thin liquid sheet 42 or 62. The preferred methodof operation is to physically touch or join the deflector plates 38 and68 together as is shown in FIG. 3. The liquid sheets 42 and 62 contactand form a new, continuous, highly-turbulent, mixed sheet 72. The mixedsheet 72 continues to thin until surface tension forces prevail, causingthe formation of droplets 73. The contacting of the sheets is in thesame general direction of liquid flow, and the contact angle 70 isusually about 30 degrees. If the liquid sheets were contacted at eachother while flowing in opposite directions, annihilation of the thinliquid sheets would occur. Further, if the angle of contact is largerthan about 60 degrees, the sheets of some liquids, particularly lowviscosity liquids such as water, have a tendency to disrupt intodroplets, rather than forming a mixed thin liquid sheet.

This preferred embodiment of the present invention has the advantagethat physical joining of deflector plates 38 and 68 ensures properalignment for mixed sheet formation at all times. Of course, thispreferred means of mixing thin liquid sheets could be initiallymanufactured as one unit.

Single thin liquid sheets of water are generally transparent. However athin mixed liquid sheet is substantially more opaque indicatingturbulence within the mixed liquid sheet. It is the combination ofcontacting two or more liquids as thin sheets and producing a highdegree of turbulence within the mixed sheet that provides for extremelyrapid mixing times. For low viscosity fluids the mixing time is of ordertenths of a millisecond, as demonstrated in Example 1, infra.

The degree of turbulence within the mixed thin liquid sheet is generallya function of the velocity of the single liquid sheets and the angle ofcontact or impingement. As the velocity and/or angle increases, so doesthe level of turbulence within the mixed sheet. In general, any angle ofcontact up to about 60° can be used for nonviscous fluids. For viscousfluids angles greater than about 30° are preferred in order to provide ahigh degree of turbulence. Further the maximum angle of contactallowable up to the point of sheet annihilation is higher for viscousfluids because the high viscosity tends to hold the liquid sheettogether.

In general, however, contact angles greater than about 60° can lead tosheet disruption with premature droplet formation. This is not apreferred method of operation for two major reasons. The droplets thatform are typically 100 times thicker than the thickness of the liquidsheet just prior to disruption. Further it is usually very difficult togenerate turbulent flow within droplets. In contrast, the preferredembodiment not only contacts two thin liquid sheets, but it alsoproduces a high degree of turbulence within the subsequently formedmixed liquid sheet.

While FIG. 3 illustrates a preferred means for practicing the presentinvention, any atomizing device that forms a thin liquid sheet, and canbe devised to impinge upon another thin liquid sheet in the same flowdirection at a gentle angle, can be used for practicing the process ofthe present invention. As shown in FIG. 4 such atomizing devices can bewhirl (or swirl) chamber-hollow cone atomizers, deflected fansprayatomizers, oval-orifice fan-spray atomizers, jet-impingement deflectedatomizers, centrifugal atomizers, rotary atomizers, rotary disc wheel orcup atomizers. These produce a sheet 18 and drops 20 similar to FIG. 1.

The preferred embodiment illustrated in FIG. 3 provides for physicalcontact between the atomizing devices. While this is highly desirablefor maintaining proper alignment and thus reliability in mixed sheetformation, it is not required for the practice of the present invention.As an example, consider atomizers 30 and 60 of FIG. 3. If deflectorplates 38 and 68 are removed, thin liquid sheets 42 and 62 will stillimpinge and form a mixed liquid sheet 72. This device, however, is lessreliable because alignment of the liquid sheets is not as easilymaintained and because the angle of contact or impingement approaches orexceeds 60 degrees since the sheet is not deflected to a 150° angle butretains about a 120° angle. These considerations are particularlyimportant in high pressure applications where vibration can causemisalignment.

Although the discussion has primarily focused on the mixing of twoliquids, tests have shown that three or more liquids may be mixedsimultaneously to produce one single mixed liquid sheet by preferredembodiments of the present invention. However, the complexity ofarranging and maintaining proper alignment may make such applicationsimpractical. A better method, depending on the fluids to be mixed, is touse the present invention in series and mix only two liquids at a time.For example, if three liquids are to be mixed, liquids 1 and 2 can bemixed by the process of the present invention. The mixture of fluids 1and 2 and the single liquid 3 can be mixed by another liquid sheet mixerin series with the first.

The present invention is applicable to any mixing process of liquidsthat can ordinarily be pumped through the liquid atomizing devices forthe production of liquid sheets. For viscous liquids this means that thefluid velocity exiting the atomizer must be at least about 0.5meter/sec; otherwise, no thin liquid sheet will form. Preferred liquidvelocities for the practice of the present invention are about 2.0meter/sec or greater. Particulate or solid matter in the fluid streamscan be handled as long as they are smaller than the smallest opening inthe atomizer so that plugging does not occur. In regards to this pointatomizers with orifices as large as 12 cm and larger can be used topractice the present invention.

The flowrates of each liquid to be mixed can be varied over quite a widerange. Liquid flowrate ratios of 10:1 have been tested, and it isbelieved that much higher ratios can be used. The important parameter ispressure drop for equal flowrates through the atomizer. The pressuredrop through each atomizer for equally viscous liquids should beapproximately the same. If widely different flowrates are desired, onesimply uses different atomizer orifice sizes. If liquids with widelydifferent viscosities are to be mixed, then the Reynolds number andvelocity of each liquid sheet are the important parameters.

The present invention is applicable to any liquid-liquid mixing processwhere the liquids in question can be formed into thin liquid sheets bythe applicable atomizing devices. It is especially applicable to fast,multiple step reactions where selectivity is a problem due to incompleteor not rapid enough mixing. An example of such an applicable process isthe coupling of 1-napthol with diazotised sulphanilic acid. The presentinvention is also very applicable to the reaction injection moldingprocess where two somewhat viscous monomers or oligmers (100 to 1000centipoise) are mixed together and react rapidly to form a highmolecular weight, high viscosity polymer that will harden in a mold.Note that because the present invention forms thin liquid sheets and athin mixed liquid sheet in free space, clogging of the atomizers andviscous product polymer buildup are not a problem.

The present invention is also very applicable to liquid-liquidextraction. Liquid-liquid extraction initially requires intimate contactbetween the light liquid phase and the heavy liquid phase. In manypractical applications, however, the dispersion of one liquid in theother is very difficult because of high interfacial tension. This canlead to overall stage efficiencies of 0.1 or less leading to many moreextraction stages than theoretically required. However, because thepresent invention contacts liquids together in thin liquid sheets andthen further mixes them turbulently within a new mixed thin liquidsheet, dispersion of the liquids is very uniform. This should increasethe overall stage efficiency for liquid-liquid extraction operations.Some other applications are fast enzyme biochemical reactions andformation of stable emulsions.

The present invention is also useful where the mixing of two liquids isaccompanied by simultaneous absorption or desorption of a gaseouscomponent. As is taught in my patent application Ser. No. 06/818,781entitled "Liquid Sheet Carbonator", filed Jan. 13, 1986, liquid sheetscan be used for the absorption or desorption of gases. The thinness ofthe liquid sheet, coupled with turbulence within the sheet, allows forrapid mass transfer and relatively high approach to equilibrium.Although a mixed sheet is typically twice as thick as a single sheet,the extremely high turbulence generated by the mixing process of thesingle sheets allows for high values of the approach to equilibrium. Theapproach to equilibrium for the mixed sheet is as high or higher thanthe single sheets. Example 3 (infra) compares the absorption of carbondioxide in a mixed liquid sheet with a single liquid sheet.

In short, the present invention is especially preferred in applicationswhere the mixing of liquids must be complete in short mixing timesand/or intimate contact between liquids is desired. Further, absorptionand/or desorption of gaseous components can occur simultaneously withthe mixing of the liquid sheets.

While the above description contains many specificities, these shouldnot be construed as limitations on the scope of the invention, butrather as an exemplification of a preferred embodiment thereof. Othervariations are possible, and these are obvious to those skilled in theart based on the principles discussed in the description.

The following examples shall serve to illustrate the practice of thepresent invention. It should be understood that the data disclosed serveonly as examples and are not intended to limit the scope of theinvention.

EXAMPLE 1 Demonstration of the Speed and Completeness with Which TotalMixing Can Be Achieved by the Present Invention

Two swirl atomizers of the type depicted in FIG. 2 producing conicalliquid sheets at a 150 degree angle were situated so that their liquidsheets produced would contact at a point about 1.3 cm from the exitingpoint of each atomizer (as in FIG. 3). The liquid sheets separately ormixed extended to a distance of about 5 to 6 cm from the atomizer, thusindicating no loss in sheet length as a result of mixed sheet formation.The angle of contact between the two single liquid sheets was 30degrees. At a distance of 1.3 cm. the single sheet thickness is about 25microns. The velocity in each liquid sheet was about 12 meter/sec,calculated as 60% of the theoretical velocity head. Sixty percent istypical of swirl atomizers of the type shown in FIGS. 2 and 3. Since thepoint at which the liquid sheets contact forms a mixed sheet of 180degrees relative to the atomizers (as in FIG. 3), there is a componentof velocity in the direction of sheet thickness. This is true becauseeach single sheet before contact flowed at an angle of 150 degreesrelative to the atomizers. The component of velocity in the direction ofsheet thickness is 12 meter/sec multiplied by the sine of one-half thecontact angle or in this case 15 degrees. Therefore, the velocity in thedirection of thickness of the mixed sheet is about 3.1 meter/sec. Sincethe thickness that the components must diffuse is only 25 microns, thephysical mixing time is about 8 microseconds.

In order to test the validity of this calculation an experiment wasdevised to estimate the time of mixing. A solution of 1.0 gmole/liter(N) NaOH containing phenolpthalein indicator was pumped through oneatomizer while a solution of 1N H₂ SO₄ was pumped through the otherswirl atomizer. It is well known that strong acid-strong baseneutralizations are virtually instantaneous. The phenolpthalein was usedas an indicator of neutralization between the acid and base. In basicsolution phenolpthalein is red, whereas it is clear in acidic solutions.However it was not possible to see the red color of the phenolpthaleinregardless of its concentration because of the extreme thinness (30microns or less) of the liquid sheets formed. To test for neutralizationa 0.5 mm probe was immersed directly into the mixed liquid sheet. Thisresulted in local premature sheet disruption along the radial line ofimmersion, causing liquid to bend up along the probe. These beads areabout 100 times or so thicker than the thin sheet and color can bereadily seen in them.

For a flowrate of 1450 milliliters/min of 1.0N NaOH containingphenolpthalein and at a contact thickness of each sheet of about 25microns, the following flowrates of H₂ SO₄ yielded the following colorof the mixed sheet:

    ______________________________________                                        1.0 N H.sub.2 SO.sub.4 flowrate                                                               Color of mixed sheet                                          ______________________________________                                         980 ml/min     red                                                           1180 ml/min     red                                                           1410 ml/min     light red                                                     1520 ml/min     clear                                                         1620 ml/min     clear                                                         ______________________________________                                    

At equal flowrates (1450 ml/min) the acid and base should neutralizeeach other, and the phenolpthalein indicator should turn clear. Allowingfor the uncertainty in the flowmeter resolution, it is seen that themixed sheet was clear when an excess of 5% acid was used. This value of5% is within the accuracy of the flowmeters used. No color was notedanywhere within the sheet at the neutralization flowrate. When the probewas immersed just beyond the well-defined mixing zone where the liquidsheets contacted, the color at the neutralization flowrate was stillclear just as it was over 5 cm further away in the mixed liquid sheet.

The time of travel 0.5 mm beyond the mixing zone for sheets with avelocity of about 12 meter/sec is approximately 4×10⁻⁵ second. Thereforethe time required for mixing yielding neutralization has a probableupper value of 40 microseconds for the low viscosity fluids tested. Thereader will note that this mixing time is less than the mixing time forKletenick's device discussed earlier. This is expected since the presentinvention contacts two liquid sheets which are thinner than the sheetsproduced by Kletenick's device. The mixing time of the present inventionis less than the mixing time claimed by Kletenick for his device, andfurther, much higher liquid flowrates can be used in the presentinvention.

EXAMPLE 2

Two swirl atomizers of the type shown in FIG. 2 producing conical sheetsat an angle greater than 150 degrees were positioned so that theirliquid sheets would contact and mix. Through both atomizers soybean oil(viscosity of about 50 centipoise) was pumped at a pressure drop of 50psi. Each sheet along was clearly in laminar flow as evidenced by theglassy appearance of the liquid sheets. When the sheets impinged, themixed sheet length actually increased by 25% from about 20 cm to about30 cm compared to the length of the single sheets.

Although the degree of turbulence in the mixed sheet was low due to thelow atomizer pressure drop and high liquid viscosity, the mixed sheetwas wavy and contained ripples of fluid. This waviness and rippling isoften used as a criterion for the onset of turbulent flow. The wavinessand rippling clearly indicate mixing in the direction of thickness ofthe mixed sheet. Higher pressure drops than that used in this example,would only serve to increase the turbulence of the mixed sheet and wouldnot effect the contacting or impingement process. Viscous fluids tend toproduce longer and more stable sheets that are more resistant todisruption than low viscosity fluids.

EXAMPLE 3 Absorption of a Gas in a Mixed Liquid Sheet

Two swirl atomizers of the type shown in FIG. 2 producing conical sheetsat an angle of about 150 degrees were positioned so that their liquidsheets would contact and mix as shown in FIG. 3. Through both atomizerswater initially free of carbon dioxide was pumped at a pressure drop of20 psi into a pressure vessel substantially containing carbon dioxide.The flowrate of water in the mixed liquid sheet was about 11.0liters/min. Water exiting the pressure vessel was found to containcarbon dioxide in an amount equal to 58% of the equilibrium or in thiscase maximum amount possible. Carbon dioxide concentration in the waterwas determined by titration with standard solutions.

When the two atomizers were positioned far apart from one another sothat a mixed liquid sheet could not form, the approach to equilibrium ofa single liquid sheet was 54%. Even though the total flowrate for themixed liquid sheet was twice as high as the single sheet, the increasedturbulence within the mixed liquid sheet allowed for a higher approachto equilibrium. The mixed liquid sheet although twice as thick as thesingle sheet, had a degree of turbulence that was much higher than theturbulence in the single sheet. Thus the reader will see that the liquidsheet mixer provides extremely rapid and uniform mixing of liquids.While the above description contains many specificies, these should notbe construed as limitations on the scope of the invention, but rather asan exemplification of one preferred embodiment thereof. Many variationson the preferred embodiment are possible. For example, as mentionedearlier, the angle of contact can vary from just greater than 0 degreesto almost 90 degrees. Accordingly, the scope of the invention should bedetermined not by the embodiment illustrated, but by the appended claimsand their legal equivalents.

I claim:
 1. A method of rapidly forming an intimate mixture of aplurality of liquids, comprising the following steps:(a) causing each ofsaid plurality of liquids to form .Iadd.in a free-space environment.Iaddend.a continuous sheet of liquid which expands in width anddecreases in thickness, (b) causing the resulting plurality of sheets ofliquid to contact each other .Iadd.in said free-space environment.Iaddend.at an acute angle and thereupon combine to form a resultantmixed sheet of said liquids, whereby said plurality of liquids willadmix with uniformity, rapidity, and intimacy.
 2. A method as in claim 1wherein each of said resulting plurality of sheets of liquid is conicalin shape.
 3. A method as in claim 1 wherein each of said resultingplurality of sheets of liquid is in the shape of a partial conicalsection.
 4. A method as in claim 1 wherein each of said resultingplurality of sheets of liquid is fan shaped.
 5. A method as in claim 1wherein each of said resulting plurality of sheets of liquid is formedby a liquid atomizing device.
 6. A method as in claim 5 wherein saidstep of forming with a liquid atomizing device comprises the use of aswirl chamber-hollow cone liquid atomizer.
 7. A method as in claim 5wherein said step of forming with a liquid atomizing device comprisesthe use of a deflected fan-spray atomizer.
 8. A method as in claim 5wherein said step of forming with a liquid atomizing device comprisesthe use of a deflected jet-impingement atomizer.
 9. A method as in claim5 wherein said step of forming with a liquid atomizing device comprisesthe use of an oval-orifice fan-spray atomizer.
 10. A method as in claim5 wherein said step of forming with a liquid atomizing device comprisesthe use of a rotary atomizer.
 11. A method as in claim 5 wherein saidstep of forming with a liquid atomizing device comprises the use of acentrifugal atomizer.
 12. A method as in claim 5 wherein said step offorming with a liquid atomizing device comprises the use of a rotarydisc atomizer.
 13. A method as in claim 5 wherein the atomizing devicesforming said resulting plurality of sheets of liquid are physicallyconnected, thereby allowing for proper alignment in the production ofsaid resultant mixed sheet of said liquids.
 14. A method as in claim 1wherein each of said resulting plurality of sheets of liquid is causedto flow laminarly and contact each other sheet so as to produce a mixedsheet of liquid in turbulent flow.
 15. A method as in claim 1 whereineach of said resulting plurality of sheets of liquid is caused to flowin a turbulent manner and contact each other sheet so as to produce saidmixed sheet of said liquids with a higher degree of turbulence than saidresulting plurality of sheets.
 16. A method as in claim 1 whereinconcurrent to forming said resultant mixed sheet of said liquids, saidresultant mixed sheet of said liquids absorbs a gaseous component.
 17. Amethod as in claim 1 wherein concurrent to forming said resultant mixedsheet of said liquids, said resultant mixed sheet of said liquidsdesorbs a gaseous component.
 18. A method of admixing a plurality ofliquids with rapidity, intimacy, and uniformity, comprising:(a) forcingeach of said liquids through an atomizer such that each of said liquidswill exit its atomizer .Iadd.into a free-space environment .Iaddend.inthe form of a continuous, thinning, conical sheet, (b) positioning eachof said atomizers so that they are coaxial and so that each faces theother atomizer and selecting the pressure, conical angle, and spacing ofsaid atomizers such that said two conical sheets will face each otherand meet .Iadd.in said free-space environment .Iaddend.at an acute angleand combine to form a resultant mixed sheet of said liquids which has acircular shape and is oriented perpendicularly to the axes of saidatomizers.
 19. A method as in claim 18 wherein said atomizers formingsaid sheets of liquid are physically connected, thereby allowing forproper alignment in production of said resultant mixed sheet of saidliquids.